CN102911683A - Carbonizing system and carbonizing process of wood materials - Google Patents
Carbonizing system and carbonizing process of wood materials Download PDFInfo
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- CN102911683A CN102911683A CN2012103758110A CN201210375811A CN102911683A CN 102911683 A CN102911683 A CN 102911683A CN 2012103758110 A CN2012103758110 A CN 2012103758110A CN 201210375811 A CN201210375811 A CN 201210375811A CN 102911683 A CN102911683 A CN 102911683A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a carbonizing system of wood materials. The carbonizing system of wood materials comprises a carbonizing device and a by-product recovery device, wherein the carbonizing device comprises a reaction vessel and a reaction chamber for putting the reaction vessel; the reaction vessel comprises a material shelf and a destructive distillation kettle for putting the material shelf; the destructive distillation kettle is composed of a destructive distillation kettle body and a destructive distillation kettle cover; an exhaust hole and a temperature measuring hole are arranged on the destructive distillation kettle cover; the reaction chamber comprises a calcining chamber with a combustion area, a carbonizing chamber, a pre-heating chamber which are sequentially arranged, a drying chamber and a cooling chamber for pre-treatment and post-treatment of wood materials respectively. The pre-heating chamber, the carbonizing chamber and/or the exhaust hole on the destructive distillation kettle cover in the calcining chamber are connected with the by-product recovery device. The system is suitable for carbonizing production of all wood materials such as tree wood, hard weed tree, bamboo material, forestry and agricultural residues (straw, shell, sawdust and on the like). The invention is scientific and rational in process, none in emission and pollution, short in production period and low in cost, thereby being suitable for popularization and application.
Description
Technical field
The present invention relates to a kind of carbonizing apparatus and technique, be specifically related to a kind of carbonization system and charring process of wood material.
Background technology
Timber or wood material generate charcoal in the situation that secluding air decomposes at a certain temperature, and by product comprises: wood tar oil, wood vinegar, wood gas.Charcoal is the impure decolorizing carbon that keeps residual tar in the original structure of timber and the hole.Be widely used as industry metallurgy reductive agent and fuel, also bringing into play significant role in fields such as purification of water quality, pollutent absorption, conduction and electromagnetic shieldings.Wood tar oil is a kind of useful product in veterinary drug, can also be as sanitas, Wood preservation agent and sealant.The composition of wood vinegar is extremely complicated, and its main component is water, acetic acid, methyl alcohol and acetone etc., mainly sprays, improves soil, body-care etc. as prevention and elimination of disease and pests, corps leaf surface.The wood gas main component is carbon monoxide, hydrogen and methane etc., and calorific value is approximately 5000kcal/m
3, be the civilian renewable and clean energy resource of alternative liquefied gas etc.Therefore, the demand of these thermal decomposition of wood products in market increases day by day.
Present charcoal is produced most local method sintering technology that adopt, and by a part of raw material of burning, makes to reach carbonization temperature, then cold stoking in the kiln in soil system or brick kiln processed.Advantage is less investment, but the shortcomings such as the charcoal quality is unstable, the production cycle long, byproduct can not reclaim, environmental pollution are arranged.
Along with the progress of science and technology, people begin to gradually adopt distillation process.Wood material is placed in the airtight Steel Shell, outside body of heater, is provided with heating furnace, by extra fuel combustion heating body of heater, the material temperature in the stove is risen, and then charing, and the pipeline collection by product by drawing.
A kind of biomass charcoal is disclosed such as Chinese patent ZL201020535353.9, gas, oil and wood vinegar cogeneration system comprise biomass retort, the vegetation raw material that fills in the biomass retort is carried out the high-temperature heater of high temperature carbonization, the gas mixture that produces in the vegetation raw material high temperature carbonization process is cooled off and the water cooling plant of gas-liquid separation and corresponding acquisition gas mixture and mixed solution, gas mixture is washed the also water washing device of corresponding acquisition wood gas, the liquid separation device that wood vinegar in the mixed solution is separated with wood tar oil, the gas-holder that wood gas is stored, water-ring vacuum pump and the compressor that joins with water-ring vacuum pump and wood tar oil storage tank and the wood vinegar storage tank that is respectively applied to store wood tar oil and wood vinegar.The shortcoming of this system is: fully the heating retort is just not emptying for the flue gas of burning, and capacity usage ratio is low; Do not have independent timber dryer, the timber still internal reaction of directly packing into has increased the energy consumption of carbonization reaction and the difficulty that byproduct reclaims.
In addition, Chinese patent ZL 200610003555.7 discloses a kind of process furnace for bamboo wood carbonized, kettle, carbonization system and charring process method, described process furnace comprises a body, the heating chamber of be positioned at body interior, be separated from each other, placing in turn, pre-charing chamber and preheating cavity; Described carbonization system comprises bamboo wood carbonized equipment, vinegar liquid recovery system and combustion gas recovery system; Described charring process method comprises that bamboo wood carbonized, vinegar liquid reclaim and combustion gas is reclaimed.This patent provides heating furnace and the novel kettle that is used for bamboo wood carbonized, avoid repeatedly heating and cooling to process furnace, saved a large amount of heating-cooling time, shortened the charing cycle, under the prerequisite of guaranteeing bamboo charcoal quality and charing efficient, production efficiency and energy utilization rate have been improved.But above-mentioned carbonization system still exists many shortcomings: conduct heat to the timber of inside by retort such as flue gas, heat exchange efficiency is low again, thereby fuel consumption strengthens, and the production cycle prolongs; Adopt the mode of naturally cooling, speed of cooling is slow, and energy does not take full advantage of etc.
Summary of the invention
The first purpose of the present invention is, for above-mentioned the deficiencies in the prior art, provides the carbonization system of the coproduction of a kind of charcoal, wood tar oil, wood vinegar and wood gas.This system is applicable to the charing production of fruit tree, hardwood, bamboo wood, all wood materials of agriculture and forestry organic waste material (stalk, shell, wood sawdust etc.).
The second purpose of the present invention is to provide a kind of technique of utilizing above-mentioned dried carbonization system wood raw material to be carried out charing.
For realizing the first purpose, the present invention adopts following technical scheme:
A kind of carbonization system of wood material comprises carbonizing apparatus and by-product plant, and described carbonizing apparatus comprises reaction vessel and is used for the reaction chamber of placing response container;
Described reaction vessel comprises material frame and is used for placing the retort of material frame; Described retort is comprised of destructive distillation kettle and destructive distillation kettle cover, and retort covers and is provided with venting port and temperature survey mouth;
Described reaction chamber comprises the calcining compartment with the combustion zone, coking chamber, the preheating chamber that sets gradually, and the kiln and the cooling room that are respectively applied to wood material pre-treatment and aftertreatment, wherein, the venting port of described calcining compartment links to each other with the inlet mouth of coking chamber by the first flue; The air outlet of described coking chamber links to each other with the inlet mouth of preheating chamber by the second flue; The air outlet of described preheating chamber links to each other with the inlet mouth of kiln by the 3rd flue; Described cooling room inlet mouth connects cool air supply duct, and the cooling room venting port links to each other with the inlet mouth of kiln by the 4th flue;
The venting port that retort covers in described preheating chamber, coking chamber and/or the calcining compartment links to each other with by-product plant.
Above-mentioned each reaction chamber is built into by refractory brick, removes retort and material frame and is prepared from by heat-resistance stainless steel.Wherein, the structure of preheating chamber, coking chamber and calcining compartment is identical, and the bottom all arranges ash discharge chamber, and links to each other successively with the second flue by the first flue.The shape of retort can make round shape, rectangle or Polygons cubes, and for ease of conducting heat, each reaction chamber also is built into the shape that is complementary with retort.
The venting port that retort covers setting is for the collection by product, and the temperature survey mouth then is to make things convenient for the user in time to detect the interior temperature of retort, accurately controls carbonization process.Mode of connection between destructive distillation kettle cover and the destructive distillation kettle is known to those skilled in the art, preferably adopts flange airtight.
The bottom all is located in the combustion zone of above-mentioned calcining compartment, coking chamber and preheating chamber, can not be as the agriculture and forestry organic waste material of charing raw material as auxiliary fuel, to realize the maximum using of resource take twig, tree root etc.In addition, its bottom also is respectively equipped with wood gas supply line and ash discharge chamber, and the wood gas supply line can provide wood gas to above-mentioned each chamber, and this wood gas forms high-temperature flue gas each chamber is heated after burning.
The inlet mouth of above-mentioned kiln also connects cool air supply duct, and the hot gas that described kiln is discharged with freezing air, preheating chamber discharge combustion product gases and cooling room is finished the drying of wood material jointly.
Described by-product plant comprises condenser, liquid separating appts, water washing device, wood tar oil storage tank, wood vinegar storage tank, wood gas storage tank, water coolant storage tank and cooling tower; Wherein condenser overhead connects water washing device, and the bottom links to each other with liquid separating appts; Described liquid fractionation plant connects respectively overstory tar storage tank, wood vinegar storage tank and understorey tar storage tank in the position of three layers of upper, middle and lowers; Described water washing device connected wood gas holder.
Described condenser is single condenser or two condenser groups that above condenser series connection arranges, and has also connected cooling tower and water coolant storage tank that water coolant is provided in order to circulation on the described condenser.In the condensation process, reduce temperature from condenser water coolant out through cooling tower, enter to drop into again behind the water coolant storage tank and recycle.
Retort of the present invention can freely pick and place in each reaction chamber, and the gap between retort and the reaction chamber consists of the inner flue of reaction chamber.Be provided with in the destructive distillation kettle inner fin and with inner fin form fit and the material frame that can freely pick and place; The external wall of described retort is provided with the outer fin that changes reaction chamber inner flue structure.
As a kind of preferred implementation of the present invention, the flue tube that is inverted L shape that can also be provided with from the bottom vertically insertion in the described destructive distillation kettle and laterally pass from the retort body side surface.
Described flue tube is 1 ~ 200, and the ratio of total cross-sectional area of flue tube and destructive distillation kettle cross-sectional area is 1/200 ~ 1/50.
Flue tube of the present invention is arranged on destructive distillation kettle middle part, and quantity can for 1 ~ 200, specifically be decided according to the size of flue tube.Satisfying total cross-sectional area of flue tube and the ratio of destructive distillation kettle cross-sectional area is 1/200 ~ 1/50, can obtain desirable heat-transfer effect.Wherein preferred flue tube is 4 ~ 10, and the ratio of total cross-sectional area of flue tube and destructive distillation kettle cross-sectional area is 1/125 ~ 2/125.
Described inverted L shape flue tube is made of vertical flue tube and the horizontal flue pipe of connection by metal hose, and specifically vertically flue tube vertically inserts from the destructive distillation autoclave body bottom, is transferring horizontal flue tube near destructive distillation kettle top and is passing from the retort body side surface.This this design can avoid temperature stress to the destruction of destructive distillation kettle and flue tube itself, thereby has prolonged whole dry distillation charring system lifetim.
Outer fin of the present invention can be for being arranged on several ring-type fins on the external wall of retort, arbitrary neighborhood two ring-type fins are respectively equipped with the breach that is staggeredly located, the interval of adjacent fins accounts for 5% ~ 100% of kettle total length, preferred 10% ~ 50%, described outer fin consists of by this breach and reaction chamber wall and revolves circuitous flue around the retort body disc.
When fuel burns in the combustion zone of reaction chamber bottom, the high-temperature flue gas that produces rises along flue, the present invention is after the external wall of retort arranges several notched ring-type fins, along the whole S-shaped rising of flue, flue gas fully contacts rear emptying from upper furnace with the destructive distillation kettle high-temperature flue gas via above-mentioned breach.Arranging of this fin increased heat interchanging area, is conducive to the charing of wood material, obtains high-quality finished product.
Above-mentioned arbitrary neighborhood two ring-type fins are equipped with the breach that is staggeredly located, the angle of two breach can be for identical or different, and be advisable preferred 90 ° ~ 180 ° to be not less than 30 °, most preferably be 180 °, this moment, high-temperature flue gas can carry out more fully heat exchange with retort.
As another embodiment of the invention, described outer fin can also be for being arranged on the spiral fin on the external wall of retort, and described spiral fin and reaction chamber wall consist of the flue around destructive distillation kettle spiral.The high-temperature flue gas that the combustion chamber produces rises along screw type flue, carries out sufficient heat exchange with the destructive distillation kettle.
In order further to optimize flue structure, improve the efficient of high-temperature flue gas and retort body heat exchange, the external fin height of contriver and reaction chamber wall to the ratio of retort outer wall spacing has also carried out specific aim research.Reaction chamber herein mainly refers to preheating chamber, coking chamber and calcining compartment.Outer fin of the present invention can perpendicular to the external wall setting of retort, also can be with it certain inclination angle and arrange.The preferred described outer fin height of the present invention is 10% ~ 100% of reaction chamber wall and retort outer wall spacing, and more preferably this ratio is 85% ~ 95%.At this moment, the flue of outer fin and reaction chamber wall, retort formation can be realized the optimization of heat transfer efficiency.
Inner fin of the present invention is several rotational symmetry distribution fins that vertically arrange on the retort inwall, and the angle of adjacent fins is 10 ~ 180 °, preferred 30 ~ 120 °.Described inner fin and retort are preferably contour.
In order to prevent the charcoal attrition crushing, guarantee simultaneously higher charring rate, the present invention has abandoned the conventional technical scheme that directly wood material is deposited in the retort, in retort, set up a material frame, material frame size and destructive distillation kettle interior shape are complementary, and are provided with 2 ~ 200 layers of flase floor, preferred 3 ~ 30 layers, more preferably 4 ~ 10 layers, flase floor is provided with the gap identical with quantity with the inner fin position.During use, wood material evenly is positioned on the flase floor of different layers, again material frame integral body is lifted up into and carry out charing in the retort, inner fin and flase floor are separated the destructive distillation kettle and are several independently spaces, not only can prevent the waste that the charcoal attrition crushing causes, can also easy-unloading, productivity is overally improved.
Those skilled in the art will know that, in the carbonization process, there is larger impact in the volumetric ratio of retort and reaction chamber to the carbonization process of wood material, this ratio is larger, illustrate that treatable wood material is more in the retort, but the too little heat transfer efficiency that causes in the space of combustion zone and flue descends, and affects productivity; This ratio is less, and the space of combustion zone and flue is larger, then more is conducive to improve heat transfer efficiency, but because the retort volume is less, will inevitably cause productive rate to descend.Hold concurrently and maximum output in order to obtain best heat-transfer effect, the contriver has made further restriction to the volumetric ratio of retort and reaction chamber, is preferably 40% ~ 96%, and more preferably 70% ~ 90%, carbonization process at this moment is the most desirable.Reaction chamber herein mainly refers to preheating chamber, coking chamber and calcining compartment.
In addition.Carbonization system of the present invention also comprises a utility appliance, and described utility appliance is lifting appliance.This lifting appliance is used at each reacting chamber space shift reaction container.
For realizing the second purpose of the present invention, adopt following technical scheme:
A kind of technique of wood material charing, described technique comprises the steps:
(1) drying; With the wood material material frame of packing into, again material frame is lifted up into kiln, pass into the mixing hot gas that is lower than the wood material burning-point from the kiln bottom it is carried out drying;
(2) preheating; Be equipped with dry after the material frame of the wood material retort of packing into, hang in preheating chamber after airtight, the high-temperature flue gas of the coking chamber of being introduced by the second flue and/or the high-temperature flue gas that base burning district fuel (comprising wood gas, twig, tree root etc.) burning produces; Or the high-temperature flue gas that high-temperature flue gas, the fuel combustion of base burning district and the wood gas supply line of the coking chamber of being introduced by the second flue produce carries out preheating;
(3) charing; The retort that preheating is complete hangs in coking chamber, retort is at the high-temperature flue gas of the calcining compartment discharge of being introduced by the first flue and/or the high-temperature flue gas of base burning district fuel (comprising wood gas, twig, tree root etc.) burning generation, or under the common heating of the high-temperature flue gas that produces of high-temperature flue gas, the fuel combustion of base burning district and the wood gas supply line of being discharged by the calcining compartment that the first flue is introduced, be warming up to 450 ~ 550 ℃, insulation charing 0.5 ~ 3h;
(4) calcining; Retort after the charing is hung in calcining compartment, under the common heating of the high-temperature flue gas that the high-temperature flue gas that is produced by base burning district fuel (comprising wood gas, twig, tree root etc.) or the fuel combustion of base burning district and wood gas supply line produce, wood material in the retort is calcined;
(5) byproduct reclaims; Collect the by product mixed gas that produces in step (2), (3), (4), pass into condenser, the product liquid that gets off through condensation enters liquid separating appts, leaves standstill, and is divided into three layers, and the upper strata accounts for 10% ~ 15%, belongs to low-boiling compound; Understorey tar accounts for 20% ~ 30%; Middle clarification partly is effective wood vinegar.Levels liquid is passed into respectively overstory tar storage tank and understorey tar storage tank, and middle layer liquid enters the wood vinegar storage tank; After passing into the water washing device washing, remove impurity, condensed gas enters the wood gas storage tank;
(6) cooling; Retort after calcining finished hangs in cooling room, passes into fresh cold air from the cooling room bottom, and after cooling finished, discharging in the retort namely got charcoal.
Wherein, the described mixing hot gas of step 1 is mixed to get by the hot gas of flue gas, step 6 generation and the discharge of step 2 generation and discharge and the freezing air that cool air supply duct provides.This mixing hot gas directly contacts with wood material.It is heated and takes away wherein moisture, emptying.The temperature of mixing hot gas in the step 1 is not higher than 150 ℃, behind dry the end, in the wood material moisture content be controlled to be≤20%.
In the step 2, the high-temperature flue gas that high-temperature flue gas, the fuel combustion of base burning district and the wood gas supply line of the coking chamber of preferably being introduced by the second flue produces is united retort is carried out preheating.By the monitoring of temperature survey mouth, the temperature of control retort inside is 210-330 ℃.Pre-thermogenetic flue gas passes into kiln via the 3rd flue.
In the step 3, under the common heating of the high-temperature flue gas that high-temperature flue gas, the fuel combustion of base burning district and the wood gas supply line that the calcining compartment of preferably being introduced by the first flue is discharged produces, retort is warming up to 450 ~ 550 ℃, insulation charing 0.5 ~ 3h, the high-temperature flue gas that this step produces passes into preheating chamber from the venting port of coking chamber via the second flue.
In the step 4, the temperature of calcining and soaking time can be according to the quality requirements of charcoal is decided, high such as charcoal fixed carbon content requirement, the temperature and time of calcining will prolong, and the high-temperature flue gas that this step produces passes into coking chamber from the venting port of calcining compartment via the first flue.
In the step 5, collect the by product mixed gas that produces in step (2), (3), (4), the venting port that covers by retort passes into condenser, cools down step by step.The product liquid that condensation is got off enters liquid separating appts, leave standstill for some time after, levels liquid passes into respectively up and down two wood tar oil storage tanks, middle layer liquid enters the wood vinegar storage tank; Pass into water washing device from the gas of condenser after out, after impurity is removed in washing, enter the wood gas storage tank.This wood gas storage tank links to each other with the wood gas supply line, passes into wood gas to the combustion chamber of calcining compartment, coking chamber and preheating chamber.The water coolant of discharging from the condenser sidewall reduces temperature through cooling tower, enters recycling behind the water coolant storage tank.
In the step 6, pass into fresh cold air from the cooling room bottom retort is cooled off, it is cooled to≤150 ℃.After cooling finished, discharging in the retort namely got charcoal.The hot gas that process of cooling produces passes into kiln via the 4th flue.
Adopt technique scheme, the invention has the advantages that:
(1) use twig, tree root etc. to become the ropy agriculture and forestry organic waste material of charcoal to be auxiliary fuel, the wood gas resource has been saved in utilization of waste material.
(2) high-temperature flue gas that produces of burning utilizes heat cascade utilization principle, by temperature from high to low, successively heating and calcining chamber, coking chamber, preheating chamber and kiln, Btu utilization is abundant.
Each heating chamber has independent base burning district and fuel inlet, can regulate respectively heating state with the temperature in the control stove.
(3) adopt the mode of forced draft cooling, both reduced the production cycle, again can be the Btu utilization of this part desiccated wood that gets up.
(4) independent Wood drying apparatus is set, by mutually directly contact of gas-solid, has greatly improved the drying efficiency of timber.And fully dry carbonization of wood speed of response is fast and even, reduces heat exhaustion.When byproduct reclaimed, condensation effect was good, reduced cooling water amount, and wood vinegar, wood tar oil purity are high.
(5) by at retort inside and outside fin being set, interior external flue has improved heat exchange efficiency, thereby reduces energy consumption, shortens the production cycle.
(6) after complete the hanging out of retort reaction that is in certain heating chamber, can hang in immediately another retort, form continuously and produce, the temperature of heating chamber is substantially constant, has saved the heating and cooling time.
(7) timber is in the airtight retort always, can not burn because touching oxygen.By the device temperature measuring apparatus, can prepare to monitor temperature of reaction, get the charcoal rate high, and steady quality.
(8) institute's by-product is all recycled, and environment is not polluted.
Description of drawings
Fig. 1 is the structural representation of the embodiment of the invention 1 dry distillation carbonizing furnace;
Fig. 2 is the A-A sectional view among Fig. 1;
Fig. 3 is material frame sectional view in the embodiment of the invention 1;
Fig. 4 is the B-B sectional view of Fig. 3;
Main figure elements explanation
1 wood gas storage tank, 2 water washing devices, 2-1 water coolant storage tank, 4 cooling towers, 5 condenser groups, 6 by product mixed gass, 7 high-temperature flue gas, 8 high-temperature flue gas, 9 destructive distillation kettle covers, 10 venting ports, 11 temperature survey mouths, 12 retorts, 13 outer fins, 14 the 4th flues, 15 material frames, 16 lifting appliances, 17 kilns, 18 hot blasts, 19 cool air supply ducts, 20 cooling rooms, 21 the 3rd flues, 22 preheating chambers, 23 ash discharge chamber, 24 second flues, 25 coking chambers, 26 calcining compartments, 27 liquid separating appts, 28 understorey tar storage tanks, 29 wood vinegar storage tanks, 30 overstory tar storage tanks, 31 wood gas supply lines, 32 first flues, 33 inner fins.
Embodiment
Below in conjunction with drawings and Examples the present invention is described further.
As shown in Figure 1, carbonization system comprises carbonizing apparatus, by-product plant and relevant utility appliance (being lifting appliance 16) in the present embodiment.
Above-mentioned carbonizing apparatus comprises reaction vessel and is used for the reaction chamber of placing response container;
Wherein reaction vessel comprises that material frame 15 reaches the retort 12 that is used for placing material frame 15; Described retort 12 is comprised of destructive distillation kettle (not indicating among the figure) and destructive distillation kettle cover 9, and destructive distillation kettle cover 9 is provided with venting port 10 and temperature survey mouth 11;
Reaction chamber comprises the calcining compartment 26 with the combustion zone, coking chamber 25, the preheating chamber 22 that sets gradually, and the kiln 17 and cooling room 20 that are respectively applied to wood material pre-treatment and aftertreatment, wherein, the venting port of calcining compartment 26 links to each other with the inlet mouth of coking chamber 25 by the first flue 32; The air outlet of coking chamber 25 links to each other with the inlet mouth of preheating chamber 22 by the second flue 24; The air outlet of preheating chamber 22 links to each other with the inlet mouth of kiln 17 by the 3rd flue 21; Described cooling room 20 inlet mouths connect cool air supply duct 19, and cooling room 20 venting ports link to each other with the inlet mouth of kiln 17 by the 4th flue 14.
In the present embodiment, by-product plant comprises condenser group 5, liquid separating appts 27, water washing device 2, understorey tar storage tank 28 and overstory tar storage tank 30, wood vinegar storage tank 29, wood gas storage tank 1, water coolant storage tank 2-1 and cooling tower 2; Wherein condenser group 5 tops connect water washing device 2, and the bottom links to each other with liquid separating appts 27; Liquid fractionation plant 27 connects overstory tar storage tank 30, wood vinegar storage tank 29 and understorey tar storage tank 28 in the position of three layers of upper, middle and lowers respectively; Described water washing device 2 connected wood gas holders 1.
As shown in Figure 2, in the present embodiment, retort inside centered by its central shaft, symmetrical uniform 6 the rectangle inner fins 33 of span centre, 60 ° of adjacent angles, its height is identical with retort.
The outer fin 13 of uniform 7 annulus of retort 12 outer short transverses of cylindrical shape, the Notch angle that two neighbouring outer fins are 13 is 180 °.
As shown in Figure 3 and Figure 4.Material frame 15 sizes and retort 12 interior shapes coupling, cylindrical, forms support by steel pipe, in the present embodiment, material frame 15 is provided with 7 layers of sub-stent, every layer of support laying grid, every layer of grid open 6 with the identical gap in inner fin 33 positions.
Embodiment 2
Compare with embodiment 1, distinctive points only is: in the present embodiment, at the middle part of retort 12, uniform 6 are inserted from the bottom, are transferring near destructive distillation kettle top laterally and the flue tube that is inverted L shape that passes from destructive distillation kettle 2 sides; The ratio of total cross-sectional area of flue tube and retort 12 cross-sectional areas is 3/200.
Embodiment 3
Compare with embodiment 1, distinctive points only is: in the present embodiment, described outer fin 13 is for being arranged on the spiral fin on the external wall of retort, and this spiral fin and each reaction chamber wall consist of the inner flue around destructive distillation kettle spiral.In the heat transfer process, high-temperature flue gas rises along the spirrillum flue, carries out heat exchange with retort.
Retort 12 inside centered by its central shaft, symmetrical uniform 4 the rectangle inner fins 33 of span centre, 90 ° of adjacent angles, its height is identical with retort.Material frame 15 is provided with 4 layers of sub-stent, and every layer of support laid grid, every layer of grid open 4 with the identical gap in inner fin 33 positions.
Embodiment 4
Compare with embodiment 1, distinctive points only is: in the present embodiment, each reaction chamber is built into rectangle by refractory brick.Retort 12 is the hollow rectangle body of high temperature resistant steel, and destructive distillation kettle cover 9 is the conical head form, and retort 12 is airtight by flange, center opened round venting port 10, and the limit is provided with gos deep into the interior thermopair of still as temperature survey mouth 11.The outer fin 13 of uniform 5 rectangular rings of retort 12 outer short transverses, the Notch angle that neighbouring two outer fins are 13 is 90 °.
Retort 12 inside centered by its central shaft, symmetrical uniform 10 the rectangle inner fins 33 of span centre, 36 ° of adjacent angles, its height is identical with retort.
Embodiment 5
The discarded limb that produces with apple tree is at first sorted as raw materials for production, and twig leaf and tree root are chosen auxiliary fuel as preheating chamber, coking chamber and calcining compartment combustion zone, and remaining is broken into length less than 30cm, and sectional area is less than 80cm
2Wooden unit.Then with the wooden unit consolidation pile up layered case screen at material frame 15, in the present embodiment, flase floor is provided with 7 layers, physical dimension and retort 12 inner chambers coupling.Material frame 15 integral body of filling are lifted up in the kiln 17 by lifting appliance 16, by about 120 ℃ hot blast 18 heat dryings approximately behind the 10h, water ratio≤20%.Dry complete after, material frame 15 is lifted up in the retort 12, in the present embodiment, retort internal diameter 1500mm, height 3000mm, 6 of inner fins, the every still approximately 2.3t that feeds.After covering kettle cover 9, hang in preheating chamber 22, the flue gas heating that the wood gas burning that is provided by auxiliary fuel and wood gas supply line 31 produces is by the monitoring of temperature measuring equipment 11, by regulating the input control combustion of wood gas and air, make the temperature of retort 12 inside be raised to approximately 270 ℃.Hanging in coking chamber 24 further heats again.Retort 12 in coking chamber 24, temperature are increased to 460 ℃ gradually, keep 1 ~ 1.5h, fully charing of wooden unit in the still is owing to the carbonization reaction in this temperature is thermopositive reaction, therefore, reduce the supply of external fuel in this step, high-temperature flue gas 7 heat supplies that main top trip calcining compartment 26 produces.Carbonization process hangs in calcining compartment 26 to retort 12 after finishing, and further is heated to 550 ℃, keeps 1 ~ 1.5h, finishes reaction, and retort 12 is hung in cooling room 20.When retort 12 being hung in next reaction chamber, successively the low retort 12 of temperature is inserted the high reaction chamber of temperature at every turn, form serialization production.Retort 12 is in cooling room 20 naturally cooling for some time at first, and the fresh cold air that passing into gradually cool air supply duct 19 provides is again forced cooling, makes temperature in the kettle be lower than 150 ℃, the discharging of uncapping.
In the above-mentioned carbonization process, the by product mixed gas 6 that retort produces in preheating chamber, coking chamber and the calcining compartment is delivered to condenser group 5 by each retort pneumatic outlet 10 respectively, in the present embodiment, condenser group 5 is that 2 condensers are in series, and can increase or reduce according to the condition of production.By product mixed gas 6 be recycled water coolant gradually the liquid that gets off of condensation enter liquid separating appts 27, liquid leaves standstill and is divided into three layers in this tank, the upper strata accounts for 10% ~ 15%, belongs to low-boiling compound; Understorey tar accounts for 20% ~ 30%; Middle clarification partly is effective wood vinegar.Levels passes into respectively overstory tar storage tank 30 and understorey tar storage tank 28, and the middle layer enters wood vinegar storage tank 29.Condenser group 5 non-condensable gas is out removed impurity after entering water washing device 2 washings, enters wood gas storage tank 1.Wood gas is incorporated into each reaction chamber (preheating chamber, coking chamber and calcining compartment) combustion heat supplying by wood gas supply line 31 from this wood gas storage tank 1.
The charcoal fixed carbon content of producing in the present embodiment approximately 78%, moisture content approximately 7%, ash content approximately 5% gets approximately 30%(over dry base of charcoal rate).
Embodiment 6
As raw materials for production, at first be broken into length less than 400mm with bamboo wood, width is less than the bamboo chip of 50mm.Then with the bamboo chip consolidation pile up layered case screen at material frame 15, in the present embodiment, flase floor is provided with 7 layers, physical dimension and retort 12 inner chambers coupling.Material frame 15 integral body of filling are lifted up in the kiln 17 by lifting appliance 16, by about 120 ℃ hot blast 18 heat dryings approximately behind the 10h, water ratio≤20%.Dry complete after, material frame 15 is lifted up in the retort 12, in the present embodiment, retort internal diameter 1500mm, height 3000mm, 6 of inner fins, the every still approximately 2.3t that feeds.After covering destructive distillation kettle cover 9, hang in preheating chamber 22, the flue gas heating that the wood gas burning that the auxiliary fuel in burned district and wood gas supply line 31 are introduced produces, monitoring by temperature measuring equipment 11, by regulating the input control combustion of wood gas and air, make the temperature of retort 12 inside be raised to approximately 300 ℃.Hanging in coking chamber 24 further heats again.Retort 12 in coking chamber 24, temperature are increased to 500 ℃ gradually, keep 1 ~ 1.5h, fully charing of bamboo chip in the still is owing to the carbonization reaction in this temperature is thermopositive reaction, therefore, reduce the supply of external fuel, high-temperature flue gas 7 heat supplies that main top trip calcining compartment 26 produces.Charing hangs in calcining compartment 26 to retort 12 after finishing, and further is heated to 700 ℃, keeps 0.5 ~ 1h, finishes reaction, again retort 12 is hung in cooling room 20 and carries out aftertreatment.When retort 12 being hung in next reaction chamber, successively the low retort 12 of temperature is inserted the high reaction chamber of temperature at every turn, form serialization production.Retort 12 is in cooling room 20 naturally cooling for some time at first, and the fresh cold air that passing into gradually cool air supply duct 19 provides is again forced cooling, makes temperature in the kettle be lower than 150 ℃, the discharging of uncapping.
In the above-mentioned carbonization process, the by product mixed gas 6 that retort produces in preheating chamber, coking chamber and the calcining compartment is delivered to condenser group 5 by each retort pneumatic outlet 10 respectively, in the present embodiment, condenser group 5 is that 2 condenser series connection arrange, and can increase or reduce according to the condition of production.By product mixed gas 6 be recycled water coolant gradually the liquid that gets off of condensation enter liquid separating appts 27, liquid leaves standstill and is divided into three layers in this tank, the upper strata accounts for 10% ~ 15%, belongs to low-boiling compound; Understorey tar accounts for 20% ~ 30%; Middle clarification partly is effective wood vinegar.Levels passes into respectively overstory tar storage tank 30 and understorey tar storage tank 28, and the middle layer enters wood vinegar storage tank 29.Condenser group 5 non-condensable gas is out removed impurity after entering water washing device 2 washings, enters wood gas storage tank 1.Wood gas is incorporated into each reaction chamber (preheating chamber, coking chamber and calcining compartment) combustion heat supplying by wood gas supply line 31 from this wood gas storage tank 1.
The bamboo charcoal fixed carbon content of producing in the present embodiment approximately 85%, ash oontent approximately 5%, iodine sorption value is 450mg approximately, gets approximately 25%(over dry base of charcoal rate).Bamboo vinegar liquid pH value 2 ~ 3, refractive index approximately 6%.
Embodiment 7
With the agriculture and forestry organic waste material (stalk, cotton seed hulls, nut-shell, sawdust etc.) that contains xylogen as raw materials for production, at first with raw material pulverizing to particle≤3mm.Then particle is layered on the layered case screen of material frame 15, the order number of the flase floor that the present embodiment is selected is larger, and flase floor is provided with 30 layers, physical dimension and retort 12 inner chambers coupling.Material frame 15 integral body of filling are lifted up in the kiln 17 by lifting appliance 16, by about 120 ℃ hot blast 18 heat dryings approximately behind the 10h, water ratio≤15%.After drying is complete, feed particles is squeezed into the rod of external diameter 50mm, internal diameter 20mm, long 400mm, density is 1.1x10 approximately
3~ 1.5x10
3Kg/m
3Again fuel rod is piled up on the material frame 15, then lifted up in the retort 12, in the present embodiment, retort internal diameter 1500mm, height 3000mm, 6 of inner fins.After covering destructive distillation kettle cover 9, hang in preheating chamber 22, the flue gas heating that the wood gas burning that the auxiliary fuel in burned district and wood gas supply line 31 are introduced produces, monitoring by temperature measuring equipment 11, by regulating the input control combustion of wood gas and air, make the temperature of retort 12 inside be raised to approximately 270 ℃.Hanging in coking chamber 24 further heats again.Retort 12 in coking chamber 24, temperature are increased to 450 ℃ gradually, keep 2 ~ 2.5h, and the fully charing of wooden unit in the still owing to the carbonization reaction in this temperature is thermopositive reaction, therefore, reduces the supply of external fuel.In the present embodiment, according to the requirement of charcoal quality product, need not carry out the calcining process of higher temperature, so finish reaction retort 12 be hung in cooling room 20.When retort 12 being hung in next reaction chamber, successively the low retort 12 of temperature is inserted the high reaction chamber of temperature at every turn, form serialization production.Retort 12 is in cooling room 20 naturally cooling for some time at first, and the fresh cold air that passing into gradually cool air supply duct 19 provides is again forced cooling, makes temperature in the kettle be lower than 150 ℃, the discharging of uncapping.
In the above-mentioned carbonization process, the by product mixed gas 6 that retort produces in preheating chamber, coking chamber and the calcining compartment is delivered to condenser group 5 by each retort pneumatic outlet 10 respectively, in the present embodiment, condenser group 5 is that 2 condenser series connection arrange, and can increase or reduce according to the condition of production.By product mixed gas 6 be recycled water coolant gradually the liquid that gets off of condensation enter liquid separating appts 27, liquid leaves standstill and is divided into three layers in this tank, the upper strata accounts for 10% ~ 15%, belongs to low-boiling compound; Understorey tar accounts for 20% ~ 30%; Middle clarification partly is effective wood vinegar.Levels passes into respectively overstory tar storage tank 30 and understorey tar storage tank 28, and the middle layer enters wood vinegar storage tank 29.Condenser group 5 non-condensable gas is out removed impurity after entering water washing device 2 washings, enters wood gas storage tank 1.Wood gas is incorporated into each reaction chamber (preheating chamber, coking chamber and calcining compartment) combustion heat supplying by wood gas supply line 31 from this wood gas storage tank 1.
The charcoal fixed carbon content of producing in the present embodiment approximately 70%, thermal value is 7000kcal/kg approximately, gets approximately 35%(over dry base of charcoal rate).
Embodiment in above-described embodiment can further make up or replace; and embodiment is described the preferred embodiments of the present invention; be not that the spirit and scope of the present invention are limited; under the prerequisite that does not break away from design philosophy of the present invention; the various changes and modifications that the professional and technical personnel makes technical scheme of the present invention in this area all belong to protection scope of the present invention.
Claims (10)
1. the carbonization system of a wood material comprises carbonizing apparatus and by-product plant, it is characterized in that:
Described carbonizing apparatus comprises reaction vessel and is used for the reaction chamber of placing response container;
Described reaction vessel comprises material frame and is used for placing the retort of material frame; Described retort is comprised of destructive distillation kettle and destructive distillation kettle cover, and retort covers and is provided with venting port and temperature survey mouth;
Described reaction chamber comprises the calcining compartment with the combustion zone, coking chamber, the preheating chamber that sets gradually, and the kiln and the cooling room that are respectively applied to wood material pre-treatment and aftertreatment, wherein, the venting port of described calcining compartment links to each other with the inlet mouth of coking chamber by the first flue; The air outlet of described coking chamber links to each other with the inlet mouth of preheating chamber by the second flue; The air outlet of described preheating chamber links to each other with the inlet mouth of kiln by the 3rd flue; Described cooling room inlet mouth connects cool air supply duct, and the cooling room venting port links to each other with the inlet mouth of kiln by the 4th flue;
The venting port that retort covers in described preheating chamber, coking chamber and/or the calcining compartment links to each other with by-product plant.
2. carbonization system according to claim 1, it is characterized in that: the inlet mouth of described kiln also connects cool air supply duct.
3. carbonization system according to claim 1 is characterized in that: described calcining compartment, coking chamber and preheating chamber are connected the bottom and are connected respectively or wood gas supply line and ash discharge chamber be set.
4. carbonization system according to claim 1, it is characterized in that: described by-product plant comprises condenser, liquid separating appts, water washing device, wood tar oil storage tank, wood vinegar storage tank, wood gas storage tank, water coolant storage tank and cooling tower; Wherein condenser overhead connects water washing device, and the bottom links to each other with liquid separating appts; Described liquid fractionation plant connects respectively overstory tar storage tank, wood vinegar storage tank and understorey tar storage tank in the position of three layers of upper, middle and lowers; Described water washing device connected wood gas holder.
5. carbonization system according to claim 1 is characterized in that: described condenser is single condenser or two condenser groups that above condenser series connection arranges, and each condenser connects respectively cooling tower and the water coolant storage tank that water coolant is provided in order to circulation.
6. carbonization system according to claim 1 is characterized in that: the inner flue of the gap formation reaction chamber between retort and the reaction chamber; Be provided with in the destructive distillation kettle inner fin and with inner fin form fit and the material frame that can freely pick and place; The external wall of described retort is provided with the outer fin that changes reaction chamber inner flue structure.
7. carbonization system according to claim 6 is characterized in that: the flue tube that is inverted L shape that is provided with from the bottom vertically insertion in the described destructive distillation kettle and laterally passes from the retort body side surface.
8. carbonization system according to claim 6, it is characterized in that: described material frame is provided with 2-200 layer flase floor, and flase floor is provided with the gap identical with quantity with the inner fin position.
9. a technique of utilizing each described carbonization system of claim 1-8 to carry out the wood material charing is characterized in that, described technique comprises the steps:
(1) drying; With the wood material material frame of packing into, again material frame is lifted up into kiln, pass into the mixing hot gas that is lower than the wood material burning-point from the kiln bottom it is carried out drying;
(2) preheating; Be equipped with dry after the material frame of the wood material retort of packing into, hang in preheating chamber after airtight, the high-temperature flue gas of the coking chamber of being introduced by the second flue and/or the high-temperature flue gas that the fuel combustion of base burning district produces; Or the high-temperature flue gas that high-temperature flue gas, the fuel combustion of base burning district and the wood gas supply line of the coking chamber of being introduced by the second flue produce carries out preheating;
(3) charing; The retort that preheating is complete hangs in coking chamber, retort is at the high-temperature flue gas of the calcining compartment discharge of being introduced by the first flue and/or the high-temperature flue gas that the fuel combustion of base burning district produces, or under the common heating of the high-temperature flue gas that produces of high-temperature flue gas, base burning district and the wood gas supply line of being discharged by the calcining compartment that the first flue is introduced, be warming up to 450 ~ 550 ℃, insulation charing 0.5 ~ 3h;
(4) calcining; Retort after the charing is hung in calcining compartment, under the common heating of the high-temperature flue gas that the high-temperature flue gas that is produced by the fuel combustion of base burning district or the fuel combustion of base burning district and wood gas supply line produce, wood material in the retort is calcined;
(5) byproduct reclaims; Collect the by product mixed gas that produces in step (2), (3), (4), pass into condenser, the product liquid that gets off through condensation enters liquid separating appts, leave standstill, levels liquid is passed into respectively overstory tar storage tank and understorey tar storage tank, and middle layer liquid enters the wood vinegar storage tank; After passing into the water washing device washing, remove impurity, condensed gas enters the wood gas storage tank;
(6) cooling; Retort after calcining finished hangs in cooling room, passes into fresh cold air from the cooling room bottom, and after cooling finished, discharging in the retort namely got charcoal.
10. technique according to claim 9 is characterized in that: the freezing air that the hot gas that the flue gas that the described mixing hot gas of step 1 is produced and discharged by step 2, step 6 produce and discharge and cool air supply duct provide is mixed to get.
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